19results about "Azeotropic/extractive distillation" patented technology

The present disclosure provides methods and systems for producing a C4+ compound, including the steps of: (i) reacting a feed stream comprising C1+O1-3 hydrocarbons in the presence of an acid condensation (AC) catalyst at a condensation temperature and condensation pressure to produce an AC product stream including the C4+ compound; (ii) fractionating AC product stream into an AC liquid product stream including organic products and a vapor stream; (iii) fractionating the AC liquid product stream by a fractionation column into a liquid C4+ compound product stream and a gaseous overhead stream; (iv) cooling the gaseous overhead stream to produce a liquid reflux stream and a gaseous vent stream; (v) recycling a first portion of the liquid reflux stream to the fractionation column for the fractionation in step (iii); and (vi) recycling a second portion of the liquid reflux stream to the feed stream for the reaction in step (i).

The utility model discloses a constant-temperature structure of aromatic hydrocarbon solvent distillation equipment, which relates to the technical field of aromatic hydrocarbon extraction and comprises a base, a heating seat fixedly connected to the upper end of the base, a constant-temperature tank fixedly connected to the upper end of the heating seat, a distillation retort arranged inside the constant-temperature tank, and a fixing frame fixedly connected to the outer surface of the distillation retort. The fixing frame is fixedly connected with the inner wall of the constant-temperature tank, a distillation outlet is formed in the upper end of the distillation tank, a feeding port is formed in the side face of the distillation tank, a liquid level control mechanism is arranged at the feeding port, a heating component and a constant-temperature module are arranged between the constant-temperature tank and the distillation tank, and a moving unit is arranged at the lower end of the base. The aromatic hydrocarbon solvent is heated and distilled through the heating component, heating is uniform, the aromatic hydrocarbon solvent is subjected to constant-temperature distillation through the constant-temperature module, and the distillation efficiency and the distillation effect are improved; and through the liquid level control mechanism, when the liquid level is low, the aromatic solvent can be automatically added, so that the influence on distillation caused by unknown distillation of the aromatic solvent or too little aromatic solvent is avoided.

The present invention relates to a Venturi separator, characterized in that the Venturi separator comprises a Venturi tube and a liquid-phase collector tube which encloses at least a part of the structure of the Venturi tube, wherein the Venturi tube comprises the following sequentially connected sections: an optional constant-diameter section, a reduced-diameter section, a neck and an expanded-diameter section, and the Venturi separator has a gas-phase inlet, a liquid-phase inlet, a liquid-phase outlet and a gas-phase outlet, wherein an opening is provided on a side wall of the expanded-diameter section of the Venturi tube or at the end of the expanded-diameter section, the opening leading to the liquid-phase collector tube so that a liquid phase can leave the Venturi tube and enter the liquid-phase collector tube under centrifugal force.The present invention also relates to the use of the Venturi separator in chemical processes.

The present disclosure provides methods and systems for producing a C4+ compound, including the steps of: (i) reacting a feed stream comprising C1+O1-3 hydrocarbons in the presence of an acid condensation (AC) catalyst at a condensation temperature and condensation pressure to produce an AC product stream including the C4+ compound; (ii) fractionating AC product stream into an AC liquid product stream including organic products and a vapor stream; (iii) fractionating the AC liquid product stream by a fractionation column into a liquid C4+ compound product stream and a gaseous overhead stream; (iv) cooling the gaseous overhead stream to produce a liquid reflux stream and a gaseous vent stream; (v) recycling a first portion of the liquid reflux stream to the fractionation column for the fractionation in step (iii); and (vi) recycling a second portion of the liquid reflux stream to the feed stream for the reaction in step (i).

A process including heating a hydrogen manufacturing unit feedstock producing a heated hydrogen manufacturing unit feedstock. The process includes stripping a wide boiling range hydrocarbon mixture with heated hydrogen manufacturing unit feedstock producing an overheads stream, separating the overheads stream to recover a non-condensed stream, and feeding the non-condensed stream to a hydrogen manufacturing unit. A process including feeding a hydrocarbon manufacturing unit feedstock to a stripping unit, recovering an overhead stream, feeding the overhead stream to a separation unit separating the hydrogen manufacturing unit feedstock from light boiling hydrocarbons, feeding a portion of the separated hydrogen manufacturing unit feedstock stream to a hydrogen manufacturing unit producing a hydrogen stream, feeding a first portion of the hydrogen stream and the bottoms stream to a first hydroprocessing unit, and feeding a second portion of the hydrogen stream, the first effluent, and the recovered medium boiling hydrocarbons to a second hydroprocessing unit.

The present application relates to an extractive distillation column comprising, from bottom to top, a tray section, a movable section and a packing section; the packing section comprises gas-liquid contact mass transfer elements referred to as first packing; the movable section comprises gas-liquid contact mass transfer elements referred to as second packing, or comprises a packing-tray composite which is a composite of gas-liquid contact mass transfer elements referred to as third packing and gas-liquid contact mass transfer elements referred to as first stereo-spray tray; the tray section comprises gas-liquid contact mass transfer elements referred to as second stereo-spray tray, wherein the extractive distillation column further comprises an extractant inlet, a feedstock inlet, a top vapor outlet, a bottom liquid outlet and optionally a side inlet, and the packing section is located above the extractant inlet; the movable section is located between the extractant inlet and the feedstock inlet; the tray section is located below the feedstock inlet. The present application also relates to an extractive distillation system comprising the above extractive distillation column and an extractive distillation method using the extractive distillation system.

The present invention concerns a process for manufacture of C6−C8 aromatic hydrocarbons from pre-sorted fractions from end-of-life vehicles (first feedstock) using at least one gasifier. Said first feedstock F1 and a second feedstock are converted in at least one gasifier into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6−C8 aromatic hydrocarbons. Next, said C6−C8 aromatic hydrocarbons are removed from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed. Next, an aromatic stream AS and a second liquid stream LR2 are removed from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6−C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6−C8 aromatic hydrocarbons.

A plant in particular for separating and purifying styrene from a crude mixture comprising styrene comprises a steam generating unit and a dividing-wall distillation column, wherein the dividing-wall distillation column comprises a dividing wall comprising a first portion extending at least essentially vertically downwards from a point being located below the top of the distillation column to a point being located above the bottom of the dividing-wall distillation column so as to subdivide the dividing-wall distillation column into a top section being located above the dividing- wall, into a bottom section being located below the dividing-wall and into a middle section comprising a first middle subsection being located on one side of the first portion of the dividing wall and a second middle subsection being located on the opposite side of the first portion of the dividing wall, wherein the dividing wall further comprises a second portion being connected with an upper part of the first portion of the dividing wall and extending into the second middle subsection to the inner wall of the dividing-wall distillation column, wherein at least a part of the bottom section extending at least over 10% of the height of the dividing-wall distillation column has a smaller cross-sectional area than the middle section of the dividing-wall distillation column, wherein the dividing-wall distillation column further comprises an inlet line for feed, an inlet line for extractive solvent, an inlet line for steam being connected with the steam generating unit, an overhead outlet line, a bottom outlet line and a side outlet line being connected with the second middle subsection of the dividing-wall distillation column, wherein the plant further comprises a side condenser and a liquid-liquid separator, wherein the side outlet line is connected with the side condenser and downstream thereof with the liquid-liquid separator, wherein the liquid-liquid separator is connected with a water line which leads into the steam generating unit.

A process for dewatering a thermochemical oil. The process comprises providing a thermochemical oil comprising water; adding a solvent selected from mesityl oxide, 2-methyltetrahydrofuran, dioxane and furfural to the thermochemical, oil, to form a mixture comprising the thermochemical oil and the solvent; heating the mixture to remove an azeotrope comprising water and the solvent from the mixture, thereby forming a dewatered thermochemical oil. A dewatered thermochemical oil. A fuel precursor.

The present invention relates to an extractive distillation column comprising, from bottom to top, a tray section, an adaptable section, and a packing section; the packing section comprises a gas-liquid contact mass transfer element, which is referred to as the first packing; the adaptable section comprises a gas-liquid contact mass transfer element, which is referred to as the second packing, or comprises a packing-tray assembly, wherein the packing-tray assembly is a combination of a gas-liquid contact mass transfer element, which is referred to as the third packing, and a gas-liquid contact mass transfer element, which is referred to as the first three-dimensional jet tray;The bottom section comprises a gas-liquid contact mass transfer element, referred to as a second three-dimensional jet tray, wherein the extractive distillation column further comprises an extraction solvent inlet, a feedstock inlet, a gas-phase outlet at the column head, a liquid-phase outlet at the column bottom, and an optional lateral piping inlet, and the packing section is located above the extraction solvent inlet; the adjustable section is located between the extraction solvent inlet and the feedstock inlet; the tray section is located below the feedstock inlet. The present invention also relates to an extractive distillation system comprising the above-mentioned extractive distillation column and to an extractive distillation process utilizing the extractive distillation system.

A plant in particular for separating and purifying styrene from a crude mixture comprising styrene comprises a steam generating unit, a liquid-liquid extraction wash column and a distillation column, wherein the distillation column comprises a top section and a bottom section, wherein at least a part of the bottom section preferably extending at least over 10% of the height of the distillation column has a smaller cross-sectional area than the top section of the distillation column, wherein the distillation column further comprises an inlet line for feed, an inlet line for extractive solvent, an inlet line for steam being connected with the steam generating unit, an overhead outlet line, a bottom outlet line and a side outlet line being arranged below the overhead outlet line and above the bottom outlet line, wherein the overhead outlet line is directly connected with the liquid-liquid extraction wash column or the overhead outlet line is directly or indirectly connected with a liquid-liquid separator comprising a water outlet line and a hydrocarbon outlet line, wherein the water outlet line is connected with the liquid- liquid extraction wash column, and the side outlet line directly connected with the liquid-liquid extraction wash column or the side outlet line is directly or indirectly connected with a liquid- liquid separator comprising a water outlet line and a hydrocarbon outlet line, wherein the hydrocarbon outlet line is connected with the liquid-liquid extraction wash column and wherein the water outlet line of the liquid-liquid separator leads into the steam generating unit.

The invention relates to a method for extractive distillation separation of a C4 alkane-alkene mixture and a composite extraction solvent, and the composite extraction solvent contains 50-90 wt% of a main solvent and the balance of a cosolvent based on the weight of the composite extraction solvent; the main solvent contains 1, 3-dimethyl-3, 4, 5, 6-tetrahydro-2-pyrimidinone, and the auxiliary solvent contains 1, 3-dimethyl-3, 4, 5, 6-tetrahydro-2-pyrimidinone. The composite extraction solvent disclosed by the invention has relatively high extraction selectivity and relatively excellent solubility when being used for separating a C4 alkane-alkene mixture.

Provided is a method for preparing synthesis gas, and more particularly, a method for preparing synthesis gas including: supplying a PFO stream including a pyrolysis fuel oil (PFO) and a PGO stream including a pyrolysis gas oil (PGO) discharged from a naphtha cracking center (NCC) process to a distillation tower as a feed stream (S10); and supplying a lower discharge stream from the distillation tower to a combustion chamber for a gasification process (S20), wherein the PGO stream is supplied to an upper end of the distillation tower and the PFO stream is supplied to a lower end of the distillation tower.

The process for producing desulfurized alpha olefins comprises reacting a hydrocarbon stream comprising conjugated diene compounds and alpha olefins in a Diels-Alder reactor at a temperature of 100°C to 250°C to form an effluent stream comprising adducts of conjugated diene compounds and alpha olefins, exposing the effluent stream to a hydrodesulfurization catalyst and a hydrogen stream in a hydrodesulfurization reactor to form the adducts, saturated C 5+ generating a hydrodesulfurization effluent stream comprising a hydrocarbon stream, and a gaseous stream; 5+ The method includes separating the hydrocarbon stream and the gaseous stream, and cracking the adducts in a first pyrolysis reactor operating at a temperature greater than 250°C to produce a cracked adduct stream comprising an alpha olefin stream and a recovered conjugated diene compound stream, wherein the gaseous stream comprises hydrogen, sulfides, C1-C4 saturated hydrocarbons, or a combination thereof.

The application discloses a limonene extraction agent in tire pyrolysis oil, wherein 30-60wt% p-aminoacetanilide and 40-70wt% quinoline are contained in the extraction agent; the extraction agent changes the interaction force between substances by itself group, and then changes the relative volatility between key components, so that the limonene product can reach more than 95% of industrial grade purity, and the yield of the limonene product also reaches more than 85%.

A process including heating a hydrogen manufacturing unit feedstock producing a heated hydrogen manufacturing unit feedstock. The process includes stripping a wide boiling range hydrocarbon mixture with heated hydrogen manufacturing unit feedstock producing an overheads stream, separating the overheads stream to recover a non-condensed stream, and feeding the non-condensed stream to a hydrogen manufacturing unit. A process including feeding a hydrocarbon manufacturing unit feedstock to a stripping unit, recovering an overhead stream, feeding the overhead stream to a separation unit separating the hydrogen manufacturing unit feedstock from light boiling hydrocarbons, feeding a portion of the separated hydrogen manufacturing unit feedstock stream to a hydrogen manufacturing unit producing a hydrogen stream, feeding a first portion of the hydrogen stream and the bottoms stream to a first hydroprocessing unit, and feeding a second portion of the hydrogen stream, the first effluent, and the recovered medium boiling hydrocarbons to a second hydroprocessing unit.

Provided is a method for preparing synthesis gas and aromatic hydrocarbons, and more particularly, a method for preparing synthesis gas and aromatic hydrocarbons including: supplying a pyrolysis fuel oil (PFO) stream containing PFO and a pyrolysis gas oil (PGO) stream containing PGO to a distillation tower as a feed stream (S10), the PFO stream and the PGO stream being discharged in a naphtha cracking center (NCC) process; and supplying a lower discharge stream from the distillation tower to a combustion chamber for a gasification process and supplying an upper discharge stream from the distillation tower to a BTX preparation process (S20).

The present invention concerns a process for manufacture of C6−C8 aromatic hydrocarbons from pre-sorted fractions of end-of-life vehicles (first feedstock) using at least one gasifier. Said first feedstock F1 and a second feedstock are converted in at least one gasifier into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6−C8 aromatic hydrocarbons. Next, said C6−C8 aromatic hydrocarbons are removed from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed. Next, an aromatic stream AS and a second liquid stream LR2 are removed from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6−C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6−C8 aromatic hydrocarbons.